CN113462427B - Method and production system for directly preparing chemicals by using crude oil and chemicals - Google Patents
Method and production system for directly preparing chemicals by using crude oil and chemicals Download PDFInfo
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- CN113462427B CN113462427B CN202110754974.9A CN202110754974A CN113462427B CN 113462427 B CN113462427 B CN 113462427B CN 202110754974 A CN202110754974 A CN 202110754974A CN 113462427 B CN113462427 B CN 113462427B
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- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
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Abstract
The invention relates to the technical field of crude oil treatment, in particular to a method and a production system for directly preparing chemicals by using crude oil and chemicals. A method for directly producing chemicals from crude oil, comprising: carrying out flash evaporation on the crude oil to obtain a light component and a heavy component; then, carrying out catalytic cracking on the heavy component to obtain a first gas component, catalytic gasoline, catalytic diesel oil, first slurry oil and first coke; carrying out catalytic cracking on the light component and catalytic gasoline to obtain a second gas component, cracked gasoline, cracked diesel oil, second slurry oil and second coke; carrying out gas separation on the first gas component and the second gas component to obtain ethylene, propylene, butylene, C2-C4 alkane and other gases; cracking the C2-C4 alkane to obtain a third gas component; the third gas component is subjected to gas separation. The method not only shortens the process flow, but also can effectively improve the conversion rate of the raw materials.
Description
Technical Field
The invention relates to the technical field of crude oil treatment, in particular to a method and a production system for directly preparing chemicals by using crude oil and chemicals.
Background
In recent years, the global oil demand is increasing continuously and is likely to be turned over in 2025 due to the influence of factors such as slow increase of economy, change of economic structure, rapid development of new energy and the like. Meanwhile, the petroleum consumption structure is changing, the petroleum ratio for producing chemical products is on the way, and the demand acceleration rate of the chemical products is far greater than that of oil products, so that the oil refining industry is deeply reformed. Under the background, the technology of directly preparing chemicals from crude oil is gradually emerging.
From the current progress of the process for preparing chemicals from crude oil, the process can be divided into 4 types.
The first is represented by the direct olefin production from exxonmobil crude oil. The process bypasses the oil refining process by feeding crude oil directly to the cracking furnace and adding a flash tank between the convection section and the radiant section of the cracking furnace. The main process comprises the following steps: the crude oil enters a flash tank after being preheated in a convection section, gas-liquid components are separated, gas-phase components enter a radiation section for cracking, and liquid-phase components are used as refinery raw materials or directly sold. The process had an ethylene yield of 26wt% and a propylene yield of 16wt%. The process has short processing flow and high chemical yield, but can only be used for processing light crude oil, and heavy components in the crude oil still need to be treated.
The second process optimizes and combines the traditional oil refining process technology to produce more chemical raw materials, and still belongs to a typical refining process. Compared with the yield of the chemical raw materials, the yield of the product oil of the process is greatly reduced by the traditional domestic refinery, and the yield of the chemicals can reach 40 percent at most. However, the process has long processing flow, many process links and relatively low chemical yield.
The third process was developed by saudi amax and saudi basic industries. The process comprises the steps of firstly sending crude oil to a hydrocracking device, then separating desulfurized lighter components and sending the separated lighter components to a traditional steam cracking device for cracking, and sending heavier components to a deep catalytic cracking device specially developed by Saudiamat to maximally produce olefin. The chemical yield of the process is close to 50%, and a large promotion space is still provided.
The fourth process is an upgraded version of the third process. Jointly developed by Saudi America, sebiye (CB & I), chevrolet Rohm Global Company (CLG). The process processes crude oil through the combined processes of deep hydrocracking, steam cracking, aromatic hydrocarbon extraction and the like, and the yield of chemical products can reach 70-80%. But the process has harsh operating conditions and higher investment cost.
In view of the above, the present invention is particularly proposed.
Disclosure of Invention
The invention aims to provide a method and a production system for directly preparing chemicals by using crude oil and chemicals. The preparation method of the embodiment of the invention not only shortens the process flow, but also can effectively improve the conversion rate of the raw materials.
The invention is realized by the following steps:
in a first aspect, the present invention provides a method for directly preparing chemicals from crude oil, comprising: carrying out flash evaporation on crude oil to obtain a light component and a heavy component;
then, carrying out catalytic cracking on the heavy component to obtain a first gas component, catalytic gasoline, catalytic diesel oil, first slurry oil and first coke;
carrying out catalytic cracking on the light component and the catalytic gasoline to obtain a second gas component, cracked gasoline, cracked diesel oil, second slurry oil and second coke;
carrying out gas separation on the first gas component and the second gas component to obtain ethylene, propylene, butylene, C2-C4 alkane and other gases;
cracking the C2-C4 alkane to obtain a third gas component;
subjecting the third gas component to gas separation.
In an alternative embodiment, the flash has a cut point in the range of 150 to 350 ℃.
In an optional embodiment, the catalyst used for catalytic cracking is any one of a molecular sieve catalyst, clay, a silicon-aluminum catalyst and a silicon-magnesium catalyst;
preferably, the catalyst used for catalytic cracking is any one of an X-type molecular sieve catalyst, a Y-type molecular sieve catalyst, a ZSM-5 molecular sieve catalyst, an M-type molecular sieve catalyst, a layered column molecular sieve catalyst, acid-treated clay, a silicon-aluminum catalyst and a silicon-magnesium catalyst;
preferably, the catalyst used for catalytic cracking is the same catalyst as the catalyst used for catalytic cracking.
In an alternative embodiment, the catalytic cracking conditions are: the reaction temperature is 440-550 ℃, the agent-oil ratio is 3-15, the reaction pressure is 0.1-0.4Mpa, the reaction time is 2-5s, and the atomized water vapor accounts for 1-8w% of the feeding amount;
preferably, the catalytic cracking conditions are: the reaction temperature is 480-530 ℃; the agent-oil ratio is 5-9; the reaction pressure is 0.15-0.35MPa; the reaction time is 2.5-4s; the atomization steam accounts for 4-6w% of the feeding amount.
In an alternative embodiment, the catalytic cracking conditions are: the reaction temperature is 550-650 deg.C, the ratio of solvent to oil is 15-30, the reaction pressure is 0.1-0.4Mpa, the reaction time is 2-5s, and the atomized water vapor accounts for 5-50w% of the feeding amount.
Preferably, the catalytic cracking conditions are: the reaction temperature is 600-650 ℃; the agent-oil ratio is 20-30; the reaction pressure is 0.1-0.3MPa; the reaction time is 3-5s; the atomization steam accounts for 30-40w% of the feeding amount.
In an alternative embodiment, the C2-C4 alkane is cracked under conditions such that: the reaction temperature is 750-850 deg.C, the reaction pressure is 0.1-0.3Mpa, the reaction time is 0.2-0.5s, and the atomized water vapor accounts for 30-80w% of the feeding amount.
Preferably, the cracking conditions of the C2-C4 alkane are: the reaction temperature is 780-820 ℃; the reaction pressure is 0.2-0.3MPa; the reaction time is 0.2-0.3s; the atomization steam accounts for 40-60w% of the feeding amount.
In an alternative embodiment, the crude oil has an S content of 0.5 to 5.0wt% and a density of 800 to 950kg/m 3 The carbon residue is 0.5-10.0wt%.
In an alternative embodiment, the method comprises the following steps: recycling the third gas component to the gas separation process of the first gas component and the second gas component;
preferably, the butylene is recycled to the catalytic cracking process of the light component and the catalytic gasoline.
In a second aspect, the present invention provides a production system for directly preparing chemicals from crude oil, comprising: a flash column for flash evaporating crude oil; heavy oil riser tube for catalytic cracking of heavy component; the second riser pipe is used for carrying out catalytic cracking reaction, the gas separation device is used for carrying out gas separation, and the cracking furnace is used for carrying out cracking;
the heavy component outlet of the flash tower is communicated with the inlet of the heavy oil riser;
the light component outlet of the flash tower and the outlet of the heavy oil riser tube, which can generate catalytic gasoline, are communicated with the inlet of a second riser tube;
the outlet of the heavy oil riser, the outlet of the second riser, and the outlet of the cracking furnace, which are capable of generating the first gas component and the second gas component, are communicated with the inlet of the gas separation device;
a butylene outlet of the gas separation device is communicated with an inlet of the second riser;
and the C2-C4 alkane outlet of the gas separation device is communicated with the inlet of the cracking furnace.
In a third aspect, the present invention provides a chemical prepared by the method for directly preparing a chemical from crude oil according to any one of the preceding embodiments.
The invention has the following beneficial effects: according to the embodiment of the invention, the specific preparation method is adopted, so that the process flow for preparing the chemicals can be effectively shortened, the conversion rate of raw materials can be effectively improved, and the yield of the chemicals prepared from crude oil can be improved.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings needed to be used in the embodiments will be briefly described below, it should be understood that the following drawings only illustrate some embodiments of the present invention and therefore should not be considered as limiting the scope, and for those skilled in the art, other related drawings can be obtained according to the drawings without inventive efforts.
FIG. 1 is a process flow diagram of a method for directly preparing chemicals from crude oil according to an embodiment of the present invention;
FIG. 2 is a schematic structural diagram of a production system for directly preparing chemicals from crude oil according to example 1 of the present invention;
reference numbers: 100-a production system; 110-a flash column; 120-a heavy oil riser; 130-a second riser; 140-a gas separation device; 150-cracking furnace.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below. The examples, in which specific conditions are not specified, were carried out according to conventional conditions or conditions recommended by the manufacturer. The reagents or instruments used are not indicated by the manufacturer, and are all conventional products available commercially.
An embodiment of the present invention provides a method for directly preparing chemicals from crude oil, which is shown in fig. 1 and includes:
carrying out flash evaporation on the crude oil to obtain a light component and a heavy component; wherein the crude oil has an S content of 0.5-5.0wt% and a density of 800-950kg/m 3 The carbon residue is 0.5-10.0wt%. The cutting point of the flash evaporation is 150-350 ℃. By adopting the cutting points, different types of crude oil can be subjected to flash evaporation, and then light and heavy components are obtained.
Then, carrying out catalytic cracking on the heavy component to obtain a first gas component, catalytic gasoline, catalytic diesel oil, first slurry oil and first coke; wherein the catalytic diesel, the first slurry and the first coke can be sold directly as an end product.
Further, the catalytic cracking conditions are as follows: the reaction temperature is 440-550 ℃, the agent-oil ratio is 3-15, the reaction pressure is 0.1-0.4Mpa (gauge pressure), the reaction time is 2-5s, and the atomized water vapor accounts for 1-8w% of the feeding amount; preferably, the catalytic cracking conditions are: the reaction temperature is 480-530 ℃; the agent-oil ratio is 5-9; the reaction pressure is 0.15-0.35MPa (gauge pressure); the reaction time is 2.5-4s; the atomization steam accounts for 4-6w% of the feeding amount. For example, the temperature may be 440 ℃, 450 ℃, 460 ℃, 470 ℃, 480 ℃, 490 ℃, 500 ℃, 510 ℃, 520 ℃, 530 ℃, 540 ℃ and 550 ℃, etc., at any value between 440 ℃ and 550 ℃, the agent-oil ratio may be 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, 13, 14 and 15, etc., at any value between 3 and 15, the pressure may be 0.1Mpa, 0.15Mpa, 0.2Mpa, 0.25Mpa, 0.3Mpa and 0.4Mpa, etc., at any value between 0.1Mpa and 0.4Mpa, the reaction time may be 2s, 3s, 4s and 5s, etc., at any value between 2s and 5s, and the atomized water vapor may account for 4w%, 4.5w%, 5w%, 5.5w%, 6w%, etc., at any value between 4w% and 6w%, etc., of the feed amount.
Further, the catalyst adopted by the catalytic cracking is any one of a molecular sieve catalyst, clay, a silicon-aluminum catalyst and a silicon-magnesium catalyst; preferably, the catalyst used for catalytic cracking is any one of an X-type molecular sieve catalyst, a Y-type molecular sieve catalyst, a ZSM-5 molecular sieve catalyst, an M-type molecular sieve catalyst, a layered molecular sieve catalyst, acid-treated clay, a silicon-aluminum catalyst and a silicon-magnesium catalyst.
The adoption of the catalyst and the catalytic cracking conditions is beneficial to the catalytic cracking reaction of the heavy oil component and the formation of the product.
Carrying out catalytic cracking on the light component and the catalytic gasoline to obtain a second gas component, cracked gasoline, cracked diesel oil, second slurry oil and second coke; the two can be catalytically cracked separately or after being mixed. Wherein, the pyrolysis gasoline, the pyrolysis diesel oil, the second slurry oil and the second coke can be used as end products and can be directly sold.
Further, the catalytic cracking conditions are as follows: the reaction temperature is 550-650 deg.C, the ratio of solvent to oil is 15-30, the reaction pressure is 0.1-0.4Mpa (gauge pressure), the reaction time is 2-5s, and the atomized water vapor accounts for 5-50w% of the feeding amount. Preferably, the catalytic cracking conditions are: the reaction temperature is 600-650 ℃; the agent-oil ratio is 20-30; the reaction pressure is 0.1-0.3MPa (gauge pressure); the reaction time is 3-5s; the atomization steam accounts for 30-40w% of the feeding amount. For example, the temperature may be 550 ℃, 560 ℃, 570 ℃, 580 ℃, 590 ℃, 600 ℃, 610 ℃, 620 ℃, 630 ℃, 640 ℃ and 650 ℃ and the like, and any value between 550 ℃ and 650 ℃, the agent-oil ratio may be 15, 17, 20, 22, 24, 25, 27, 29 and 30 and the like, any value between 15 and 30, the pressure may be 0.1Mpa, 0.15Mpa, 0.2Mpa, 0.25Mpa, 0.3Mpa and 0.4Mpa and the like, any value between 0.1Mpa and 0.4Mpa, the reaction time may be 2s, 3s, 4s and 5s and the like, and any value between 2 and 5s, and the atomizing water vapor may account for 5w%, 10w%, 25w%, 30w%, 35w%, 40w%, 48w% and the like, and any value between 5 and 50w% of the feed amount.
The catalyst used for catalytic cracking and the catalyst used for catalytic cracking are the same catalyst. It will of course be appreciated that the catalysts may not be identical.
The adoption of the catalyst and the catalytic cracking conditions is beneficial to catalytic cracking of light components and obtaining of terminal products.
Carrying out gas separation on the first gas component and the second gas component to obtain ethylene, propylene, butylene, C2-C4 alkane and other gases; the first gas component and the second gas component may be mixed for gas separation or may be separated separately. Among these, ethylene, propylene and other gases are end products.
The butylene can be obtained by further catalytic cracking, and the catalytic cracking conditions are the same as those of the light component and the catalytic gasoline, namely the butylene can be recycled to the light component and the catalytic gasoline for catalytic cracking.
Wherein, C2-C4 alkane is cracked to obtain a third gas component rich in ethylene and propylene; and the third gas component may be further subjected to gas separation, where the gas separation may be a gas separation by recycling the third gas component to the first gas component and the second gas component.
In summary, the embodiment of the invention can select the optimal cutting temperature for different types of raw materials, respectively process heavy components, light components, catalytic gasoline and butylene of crude oil by utilizing the flexible and multiple-effect characteristics of catalytic cracking and catalytic cracking, and simultaneously match the optimal process flow and operation conditions to maximally produce chemicals. On the basis, the embodiment of the invention excavates the potential of converting catalytic cracking products into chemicals, and pertinently introduces the low-carbon alkane cracking furnace to process C2-C4 alkanes, thereby realizing the optimal solution of processing crude oil to prepare chemicals and maximizing the conversion rate of the raw material to the chemicals. In order to save energy consumption and reduce the construction cost of the device, the catalytic cracking device and the cracking furnace share one set of gas separation system. Under the optimized process condition, the yield of the crude oil chemical product is not lower than 70% by utilizing two sets of reaction devices. In conclusion, the method has the advantages of strong raw material adaptability, high utilization rate, low equipment investment and production cost, high chemical yield and the like.
The embodiment of the invention provides a chemical product, which is prepared by the method for directly preparing the chemical product by using crude oil.
It should be noted that the references to first, second, third, etc. in the embodiments of the present invention do not denote any order or importance of the product, but merely serve to distinguish the nomenclature of the chemicals.
The features and properties of the present invention are described in further detail below with reference to examples.
Example 1
The embodiment of the invention provides a production system 100 for directly preparing chemicals by using crude oil, which comprises a flash tower 110 for carrying out flash evaporation on the crude oil; that is, the crude oil is introduced into the flash column 110 to be flashed, and then the light component and the heavy component are obtained.
The production system 100 also includes a heavy oil riser 120 that catalytically cracks heavy components; the heavy component outlet of the flash tower 110 is communicated with the inlet of the heavy oil riser 120; then, the heavy component can enter the heavy oil riser 120 to perform a catalytic cracking reaction, so as to form a first gas component, catalytic gasoline, catalytic diesel oil, first slurry oil and first coke.
The production system 100 further comprises a second riser 130 for performing catalytic cracking reaction, and both the light component outlet of the flash tower 110 and the outlet of the heavy oil riser 120 capable of generating catalytic gasoline are communicated with the inlet of the second riser 130; the light components and the catalytic gasoline can then undergo a catalytic cracking reaction in the second riser 130 to form a second gas component, pyrolysis gasoline, pyrolysis diesel, a second slurry oil, and a second coke.
The production system 100 further comprises a gas separation device 140 for gas separation, and an outlet of the heavy oil riser 120 capable of generating a first gas component and an outlet of the second riser 130 capable of generating a second gas component are both communicated with an inlet of the gas separation device 140; the first gaseous component and the second gaseous component can then undergo gas separation and form ethylene, propylene, butylene, C2-C4 alkanes, and other gases.
The production system 100 further includes a cracking furnace 150 for performing cracking; the C2-C4 alkane outlet of the gas separation device 140 is communicated with the inlet of the cracking furnace 150, so that the C2-C4 alkane can be subjected to cracking reaction to form the third gas component, and meanwhile, the outlets of the cracking furnace 150 capable of generating the third gas component are communicated with the inlet of the gas separation device 140; the third gas component may then be subjected to gas separation.
Example 2
The present embodiment provides a method for directly preparing chemicals by using crude oil, which is implemented by using the production system 100 for directly preparing chemicals by using crude oil provided in example 1, specifically:
the crude oil passes through a flash column 110 and is cut into light and heavy components. Wherein the heavy component goes to the heavy oil riser 120 for catalytic cracking and the light component goes to the second riser 130 for catalytic cracking. The heavy component is processed by a heavy oil riser 120 to generate a first gas component, catalytic gasoline, catalytic diesel oil, first slurry oil and first coke, wherein the catalytic gasoline is fed to a second riser 130; processing the light component by a second riser 130 to generate a second gas component, pyrolysis gasoline, pyrolysis diesel, second slurry oil and second coke; separating the first gas component and the second gas component into ethylene and propylene products, butylene and C2-C4 alkane through a gas separation device 140, wherein the butylene is sent to a second riser 130, and the C2-C4 alkane is sent to a cracking furnace 150; the third gas component produced by processing the C2-C4 alkane through the cracking furnace 150 is passed to the gas separation unit 140.
The crude oil properties are shown in Table 1, the main operating conditions are shown in Table 2, and the products of the whole process are shown in Table 3.
Example 3
This example provides a method for directly preparing chemicals from crude oil, which is similar to the method provided in example 2, except that the type of crude oil processed is different and the cutting temperature of the flash tower is different. The crude oil properties are shown in Table 1, the main operating conditions are shown in Table 2, and the total product flow is shown in Table 3.
Example 4
This example provides a method for directly preparing chemicals from crude oil, which is similar to the method provided in example 2, except that the type of crude oil processed is different and the cutting temperature of the flash tower is different. The crude oil properties are shown in Table 1, the main operating conditions are shown in Table 2, and the total product flow is shown in Table 3.
TABLE 1 crude oil Properties
TABLE 2 Main operating conditions
TABLE 3 full run product distribution
Note: in Table 3, the aromatic hydrocarbon means: the amounts of aromatics in pyrolysis gasoline, pyrolysis diesel and catalytic diesel refer to the amounts of aromatics free of the corresponding oil fractions.
As can be seen from Table 3, the method for directly preparing chemicals from crude oil provided by the embodiment of the invention has strong adaptability to different types of crude oil, and the yield of chemicals can reach about 70wt% by matching optimal operating conditions for different types of crude oil.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (7)
1. A method for directly preparing chemicals by using crude oil is characterized by comprising the following steps: carrying out flash evaporation on the crude oil to obtain a light component and a heavy component; the cutting point of flash evaporation is 150-350 ℃;
then, carrying out catalytic cracking on the heavy component to obtain a first gas component, catalytic gasoline, catalytic diesel oil, first slurry oil and first coke;
carrying out catalytic cracking on the light component and the catalytic gasoline to obtain a second gas component, cracked gasoline, cracked diesel oil, second slurry oil and second coke;
carrying out gas separation on the first gas component and the second gas component to obtain ethylene, propylene, butylene, C2-C4 alkane and other gases;
cracking the C2-C4 alkane to obtain a third gas component;
subjecting the third gaseous component to gas separation;
the catalyst adopted by catalytic cracking is any one of a molecular sieve catalyst, argil, a silicon-aluminum catalyst and a silicon-magnesium catalyst; the catalyst used for catalytic cracking and the catalyst used for catalytic cracking are the same;
the crude oil has an S content of 0.5-5.0wt% and a density of 800-950kg/m 3 0.5-10.0wt% of carbon residue;
the catalytic cracking conditions were: the reaction temperature is 440-550 ℃, the agent-oil ratio is 3-15, the reaction pressure is 0.1-0.4MP a, the reaction time is 2-5s, and the atomized water vapor accounts for 1-8w% of the feeding amount;
the catalytic cracking conditions are as follows: the reaction temperature is 550-650 ℃, the agent-oil ratio is 15-30, the reaction pressure is 0.1-0.4MP a, the reaction time is 2-5s, and the atomized water vapor accounts for 5-50w% of the feeding amount;
the cracking conditions of the C2-C4 alkane are as follows: the reaction temperature is 750-850 ℃, the reaction pressure is 0.1-0.3MP a, the reaction time is 0.2-0.5s, and the atomized water vapor accounts for 30-80w% of the feeding amount.
2. The method for directly preparing chemicals from crude oil according to claim 1, wherein the catalyst used in the catalytic cracking is any one of an X-type molecular sieve catalyst, a Y-type molecular sieve catalyst, a ZSM-5 molecular sieve catalyst, an M-type molecular sieve catalyst, a layered column molecular sieve catalyst, an acid-treated clay, a silica-alumina catalyst and a silica-magnesium catalyst.
3. The method for directly preparing chemicals by using crude oil as claimed in claim 1, wherein the conditions of catalytic cracking are: the reaction temperature is 480-530 ℃; the agent-oil ratio is 5-9; the reaction pressure is 0.15-0.35MPa; the reaction time is 2.5-4s; the atomization steam accounts for 4-6w% of the feeding amount.
4. The method for directly preparing chemicals from crude oil according to claim 1, wherein the catalytic cracking conditions are as follows: the reaction temperature is 600-650 ℃; the agent-oil ratio is 20-30; the reaction pressure is 0.1-0.3MPa; the reaction time is 3-5s; the atomization steam accounts for 30-40w% of the feeding amount.
5. The method for directly preparing chemicals from crude oil according to claim 1, wherein the cracking conditions of the C2-C4 alkane are as follows: the reaction temperature is 780-820 ℃; the reaction pressure is 0.2-0.3MPa; the reaction time is 0.2-0.3s; the atomization steam accounts for 40-60w% of the feeding amount.
6. The method for directly producing chemicals from crude oil according to any of claims 1 to 5, comprising: recycling the third gas component to the gas separation process of the first gas component and the second gas component.
7. The method for directly preparing chemicals by using crude oil according to claim 6, wherein the butene is recycled to the catalytic cracking process of the light components and the catalytic gasoline.
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